Antibiotic production utilizing streptomyces refuineus var. thermotolerans

ABSTRACT

Antibiotics having antitumor and antibacterial activity are produced by fermentation of thermophilic actimomycetes Streptomyces refuineus var. thermotolerans, having NRRL numbers 3,143 and 3,144, in a nutrient medium containing a protein source and a carbohydrate source, at 35* C. to 55* C., extracting the fermentation broth with a solvent and isolating the active fraction.

United States Patent [72] Inventors Julius Berger Passaic; Andrew E. Karr, Bloomfield; Willy Leimgruber, Montclair; Benjamin Tabenkin, Upper Montclalr, N.,].; Arno Johannes Schocher, Benken, Switzerland; Vladimir Stefanovic, Needham, Mass.

[211 App]. No. 687,433

[22] Filed Dec. 4, i967 [23] Division of Ser. No. 416,599, Dec. 7,

1964, Pat. No. 3,361,742

[45] Patented Nov. 9, 1971 [73] Assignee Hottmann-La Roche Inc.

Nutley, NJ.

[54] ANTIBIOTIC PRODUCTION UTILIZING STREPTOMYCES REFUINEUS VAR.

[50] Field of Search l95/80 5 6] References Cited OTHER REFERENCES Tendler, South African Complete Specification, No. 3875, Aug. 26, 1963, 6 260/2393 Lit.

Nature, Vol. 199, No. 4892, Aug. 3, 1963, pg. 501, Copy in Sci. Library.

Levine et al., A Compilation of Culture Media, 1930, Williams & Wilkins Co., Baltimore, pg. 377, Copy in Art Unit 172.

Primary Examiner-Joseph M. Golian Attorneys-Samuel L. Welt, Jon S. Saxe, William H. Epstein, Gerald S. Rosen, Bernard S. Leon, William G. lsgro and Jacob Frank ABSTRACT: Antibiotics having antitumor and antibacterial activity are produced by fermentation of thermophilic actimomycetes Slreptomyces refuineus var. rhermotolerans, having NRRL numbers 3,143 and 3,144, in a nutrient medium containing a protein source and a carbohydrate source, at 35 C. to 55 C., extracting the fermentation broth with a solvent and isolating the active fraction.

ANTIBIOTIC PRODUCTION UTILIZING STREP'IOMYCES REFUINEUS VAR. THERMOTOLERANS This application is a division of copending US. Pat. application, Ser. No. 416,599, filed Dec. 7, 1964 by Berger et al. and now US. Pat. No. 3,361,742.

BACKGROUND OF THE INVENTION It is known that the cultivation of certain thermophilic actimomycetes results in the production of a fermentation broth having anticancer activity (see, e.g., South African application No. 63/3975).

SUMMARY OF THE INVENTION DETAILED DESCRIPTION OF THE INVENTION The above strains of Streptomyces refiuneus var. thermotolerans have the following taxonomic description:

Substrate mycelium branched, 0.5 to 0.74 in diameter. Growth at first white, progressing to medium yellow, yelloworange, or medium tan; or white, changing to gray, gray-green (near grey k fe) (Descriptive Color Names Dictionary, Container Corporation of America), olive or black. Aerial mycelium moderate to abundant, powdery or sometimes cottony, white, cream-yellow, or medium gray to deep gray-green (near gray 24% ml.), depending on the medium composition. Sporphores monopodially branched, with numerous open extended or compact spirals, the latter occurring infrequently; spirals usually with one to four coils, sometimes up to eight to turns. Spores oval, short to elongated, irregularly rough to warty, 0.5 to 1.2 by 1.0 to 2.3;1. Mycelium and spores grampositive, not acid-fast. Vegetative mycelium lysozyme sensitive. Soluble pigment produced in several media. Facultative thermophile. Habitat: donkey dung.

In the specification, the color designations in parenthesis are according to Descriptive Color Names Dictionary, Container Corporation of America.

GROWTH CHARACTERISTICS Procedure:

The inoculum for culture studies was developed in shaken flasks for l4-6 hours at 45 C., in the medium 0.5% BACTO- TRYPT ONE plus 0.3% BACTO yeast extract to volume with distilled water.

The instant strains were grown at 45 C. for about 2 days, unless otherwise stated, before their culture characteristics were determined. Cultures were then reincubated for an additional period of 3 to 10 days to observe if any further changes occurred.

The following media designations are taken from Applied Microbiology 9: 394-399 1961).

MAINTENANCE MEDIUM Ia NRRL 3143 Growth thin, white to gray. Aerial mycelium moderate, white to light gray.

NRRL 3144 Growth good, white to deep gray. Aerial mycelium abundant, white to cream-yellow to light gray.

MEDIUM Ib NRRL 3143 Growth abundant, white to light gray, later deep gray-black. Aerial mycelium moderate, thin, "white to medium gray-green.

NRRL 3144 Growth abundant, white to medium gray, changing to deep gray. Aerial mycelium abundant, cottony, white, later gray-green.

MEDIUM II NRRL 3143 Growth good, pale gray changing to deep gray. Aerial mycelium abundant, light gray to medium gray.

NRRL 3144 Growth good, medium to deep gray. Aerial mycelium light gray, changing to medium gray, then greenishgray.

MEDIUM III NRRL 3143 Growth moderate, restricted, white to pale gray. Aerial mycelium scant, appearing late, white to light gray.

NRRL 3144 Growth good, white to pale cream-yellow. Aerial mycelium scant, white to cream-yellow, later light gray.

MEDIUM IV NRRL 3143 Growth thin, white to light gray. Aerial mycelium light gray to medium gray.

NRRL 3144 Growth thin, white to cream-yellow, later light gray. Aerial mycelium cream-yellow to light gray.

MEDIUM V NRRL 3143 Growth good, white then gray to light brown. Aerial mycelium thin, white at first, later pale gray-green. Soluble pigment light brown.

NRRL 3144 Growth good, white, later cream-yellow to light brown. Aerial mycelium thin, white to cream-yellow, changing to light gray-green. Soluble pigment light brown.

MEDIUM VI NRRL 3143 Growth good, relatively thick, light gray, later changing to dark gray-green. Aerial mycelium abundant, cottony, light gray, becoming light gray-green. Soluble pigment yellow, later tan, light yellow reverse.

NRRL 3144 Growth abundant, thick, medium gray to graygreen (near gray 24% fe). Aerial mycelium medium gray, later becoming gray-green (near gray 24% ml.). Soluble pigment yellow, later tan, light yellow reverse.

MEDIUM VII NRRL 3143 Growth very thin, creeping, light gray. Aerial mycelium scant, white to light gray.

NRRL 3144 Growth thin, creeping, light gray. Aerial mycelium scant, light gray.

TOMATO OATMEAL No growth with either culture at 28 C. or at 45 C.

AMIDEX NRRL 3144; 45 C.Growth abundant, white to lemonyellow, later dark olive. Aerial mycelium white to cream, becoming light gray. Soluble pigment light tan.

NRRL 3144; 28 C.Growth abundant, white to pale yellow, changing to mustard tan. Aerial mycelium moderate, light gray. No soluble pigment.

NRRL 3143; 45 C.Growth abundant, white to light gray, changing to dark olive. Aerial mycelium white to light gray. Soluble pigment light tan.

NRRL 3143; 28 C.--Growth moderate, white, later camel (3 i.e.). Aerial mycelium scant, white. No soluble pigment.

CZAPEK-GLUCOSE NRRL 3144; 45 C.Growth scant, white to pale yellow. Aerial mycelium sparse, white. No soluble pigment.

NRRL 3144; 28 C.Growth fair, white to ivory, then medium olive. Aerial mycelium scant, white No. soluble pigment.

NRRL 3143; 45 C. -Growth very poor, white, Aerial mycelium scant, white. No soluble pigment.

NRRL 3143; 28 C.Growth fair, white to pale yellow. Aerial mycelium scant, white. No soluble pigment.

YEAST AND MALT EXTRACT NRRL 3144; 45 C.Excellent growth, white to pale yellow. Aerial mycelium white to cream. Soluble pigment pale yellow.

NRRL 3144; 28 C.Abundant growth, white to pale yellow or medium olive. Aerial mycelium white to medium gray. No soluble pigment.

NRRL 3143; 45 C.Growth abundant, white to pale orange-yellow. Aerial mycelium white, mealy. Soluble pigment light yellow.

NRRL 3143; 28 C.Growth abundant, white to light yellow. Aerial mycelium moderate, white. No soluble pigment.

GLUCOSE-NUTRIENT NRRL 3144; 45 C.Growth scant, white to cream-yellow. Aerial mycelium trace, white, Soluble pigment not observed.

NRRL 3144; 28 C.Growth moderate, white to pale yellow. Aerial mycelium scant, white. No soluble pigment.

NRRL 3143; 45 C.Growth scant, white to pale yellow. Aerial mycelium trace, white. N soluble pigment.

NRRL 3143; 28 C.-Growth good, white to pale yellowbrown. Aerial mycelium scant, white. No soluble pigment.

GLUCOSE-NUTRIENT GLYCEROL NRRL 3144; 45 C.Excellent growth, white to pale orange-yellow. Aerial mycelium sparse, white. Soluble pigment pale orange-yellow.

NRRL 3144; 28 C.Growth moderate, white, later golden yellow. Aerial mycelium scant, white. No soluble pigment.

NRRL 3143; 45 C.Growth abundant, white or pale yellow-orange. Aerial mycelium scant, white. Soluble pigment pale orange-yellow.

NRRL 3143; 28 C.Growth moderate, white to golden yellow, then tan. Aerial mycelium scant, white. No soluble pigment.

P AND G DEXTRIN NRRL 3144; 45 C.Growth scant, white to pale yellow. Aerial mycelium powdery, white. No soluble pigment.

NRRL 3144; 28 C.Growth scant, white to pale yellow, later medium olive. Aerial mycelium moderate, white. Trace of pale yellow soluble pigment.

NRRL 314345 C.Growth moderate, white to cream. Aerial mycelium white, powdery. No soluble pigment.

NRRL 3143; 28 C.Growth scant, white to light yellow. Aerial mycelium poor, white. Trace of pale yellow soluble pigment.

GLUCOSE ASPARAGINE NRRL 3144; 45 C.-Growth very sparse, white. Aerial mycelium scant, white. No soluble pigment.

NRRL 3144; 28 C.--Growth fair, white to pale cream-yellow. Aerial mycelium moderate, powdery, white. No soluble pigment.

NRRL 3143; 45 C.Growth scant, white to cream. Aerial mycelium trace, white. No soluble pigment.

TYROSINE TEST Test tom parature, C.

Aerial Color of Culture Growth mycelium reverse 7 Scant...

. Scent None"... Ivory Pale yellow- NRRL 3144..

NRRL 3143.

D- D- ant-rebut 65PM, I i I I C olor pigment NRRL 3143; 28 C.Growth poor, white to cream-yellow. Aerial mycelium scant, white. No soluble pigment.

STARCH SKlM MILK NRRL 3144; 45 C.Growth scant, white to pale yellow. Aerial mycelium scant, white. Hydrolysis good. Light brown soluble pigment.

NRRL 3144; 28 C.Growth moderate, white to pale yellow. Aerial mycelium, thin, white. Hydrolysis good. Light tan, soluble pigment.

NRRL 3143; 45 C.Growth scant, white to pale yellow. Aerial mycelium sparse, white. Hydrolysis good. Pale brown, soluble pigment.

NRRL 3143; 28 C.Growth fair, white to light yellow. Aerial mycelium sparse, white. Hydrolysis good. Trace pale brown, soluble pigment.

BENNE'IT'S AGAR NRRL 3144; 45 C.Growth excellent, white to pale yellow-orange, later medium tan. Aerial mycelium sandy to light gray. Trace of yellow, soluble pigment.

NRRL 3144; 28 C.Growth moderate, white to pale yellow. Aerial mycelium white. No. soluble pigment.

NRRL 3143; 45 C.--Growth moderate, white to pale yellow, later medium tan. Aerial mycelium scant, white. Trace of soluble pale yellow pigment.

NRRL 3143; 28 C.Growth excellent, white at first, later cream-yellow. Aerial mycelium abundant, white. No soluble pigment.

CARROT PLUG AND POTATO PLUG NO growth was observed with either strain at 28 C. or 45 C.

METABOLIC ACTlVlTlES HYDROGEN SULFIDE TEST (BACTO PEPTONE IRON AGAR) No H s was produced by either strain at 28 C. or at 45 C.

Growth of NRRL 3144 and NRRL 3143 was relatively poor on the peptone-iron agar. NRRL 3144 produced yellow to olive growth; aerial mycelium scant, white to gray. NRRL 3143 produced pale yellow growth but no aerial mycelium.

None

Pale salmon.

Light beige.

.. Pale salmon.

Light vinaceous. Light tea brown.

Pale salmon. Light beige. Pale flesh.

Pale salmon. Fawn.

No liquefaction of gelatin was observed at 28 C. or at 45 C. with either culture. All inoculated gelatin tubes were incu- The fermentation process of the invention is carried out by culturing one of the above organisms in a nutrient medium. The characteristics of the nutrient media are highly important for obtaining good yields of the antibiotic of the invention. In

bated for 10 days at 45 C. or 14 days at 28 C. But high- 5 particular, the nutrient media must have the following characproteolytic activity vs. many proteins was observed on comteristics in order to give good antibiotic yields: plex media.

ACTION ON MILK Tem- Day perao1 ture, roud- Coagu- Popto- Culture 0. ing lotion iilzntlon Growth llgiiii-iit.

28 2 0 0 0. 28 7 l) Slight. light yollow 0. 28 14 0 do ii. NRRL Z? 1 :13; 0. 45 2 0 0. 415 4 o Light blego. 45 5 Vlslblo on rlng Do. 28 2 0 0 0 0. 28 7 0 0 Trace llght yellow. 0. 28 21 NRRL 3143.. Z2 g g;

45 4 1 Light blego.

light yellow. 45 5 +(25%) ..do Do.

1 Incomplete.

NITRATE REDUCTASE ACTIVITY CARBON UTlLlZATlON TEST ORGANIC BROTH 0 m Oh lnW scrvatirms NRRL 3144; 45 C.Surface and submerged growth NRRL NRRL I Compound 211 C. 45" C. 28 C. 45 C. recorded in 48 hours; no nitrate reduction observed after 6 days.

x l NRRL 3l44; 28 C.Surface and submerged growth obx i I 1 served in 7 days; no nitrate reduction observed after 14 days. Rhamnosc +1 H NRRL 3143; 45 C.Surface and submerged growth Demo +(-H') developed in 48 hours; no nitrate reduction observed in 6 E accharose y Lactose NRRL 3143; 28 C.-Submerged growth observed in 7 R ffinose days; no nitrate reduction after 14 days. :28? r 40 Multose H-H-y L H) L, Inorganic Broth Munniml g s NRRL 3144; C.Light submerged growth observed in 3:53 4 days; no nitrate reduction after 6 days. Galactose H 2 H NRRL 3144; 28 C.Surface and submerged growth Mumfosc +i++i recorded in 7 days; no nitrate reduction after 14 days. 45 grl li b it ise Iu-w :H-H lH-r E d NRRl. j 143, 45 C.No visible growth detected during 6- new, RH) H H 8} perio Starch NRRL 3143; 28 C.Some submerged growth recorded in T' I H-H I P eno 7 days, no nitrate after 14 days. Nwceme I Na-citrate z NlTROGEN UTILIZATION TEST Nmmcinm z t Growth Observations NRRL 3144 NRRL 3143 Tcst Compound 28 C. 45 C. 28 C. 45 C. Explanation ofsignsz growthlike control, i.e., with (NH),SO. but without NuNQ +H-H +(-H-) +(-H-) carbon source (NHJZSO. 1 P growth NH -acetatc poor to fair growth Incubation time: Asparaginc -H- -i+ +4- +(-H-) fair growth 45 C.- hours i i +1- good growth 28 C.l00 hours Betainc HCI a-uminoisobutyric acid 1 t Crcatinc 1- -H- H Sudium glutamate HM) H HH) +(H) 1. From about 0.1 to about 9.0, preferably from about to Glycine about 5.0 percent by weight of complex protein-containing i 14H) (+1 5 products, in the final nutrient medium. The protein source 1 1 1 1 should have a ratio of total nitrogen to amino nitrogen greater Tryptophunc than three and the total nitrogen in the medium should be in Tyrosine the range of from about 0.005 to about 0.48, preferably from f about 0.015 to about 0.20 percent w/v. Examples of protein Gelatin Egg albumin sources that answer the above requirements include milk products, e,g., peptonized milk or dried milk, skim milk, etc.; Explanation of signs: enzyntilzttic dz gests of soy, yeast, fish or peanut proteins, or mixgrowthlikc control, i.c., with glucose but without tures ereo nitrogen solurcc 2. A carbohydrate source. The quantity of carbohydrate pour growl Incubation time:

45 (1-65 hours 28 C.-l00 hours poor to fair growth fair growth -H- good growth does not appear to be too significant and is generally in the range of from a out 0.25 to about 11.5 percent w/v. Carbohydrate sources that can be employed include alcohols, su-

gars and crude or purified starches, e.g., corn starch, potato starch, soluble starches, glycerol, mannitol, lactose, maltose, etc.

3. The initial pH of the fermentation broth must be in the range of from about 6 to about 8.5, preferably from about 6.7 to about 7.3. After about 12 to about 15 hours of fermentation, the pH is maintained thereafter in the range of about 6.0 to about 6.9, e.g., by the addition of an alkali metal hydroxide, e.g., sodium hydroxide, or by sulfuric acid.

Also, there can be added up to about 2.5 percent of dried yeast or yeast extract to the basal medium. However, this is an optional ingredient.

The fermentation is carried out by forming a nutrient medium as described above, sterilizing it, e.g., at 120 C. for 15 to 20 minutes, and then inoculating the nutrient medium either with spores or vegetative growth of one of the above organisms and permitting the fermentation to proceed with agitation and aeration at a temperature in the range of from about 35 to about 55, preferably from about 40 to about 50 C. and from about to about 100, preferably about 12 to about 30 hours.

The fermentation broth is then optionally filtered, and extracted with an extraction solvent, preferably in two extraction steps.

Extraction solvents that can be employed in both extraction steps include (a) a solvent comprising a monohydric saturated aliphatic alcohol having a boiling point up to about 200 C. which has a low-miscibility (e.g., less than 25 percent) with cold water, e.g., n-butanol, isobutanol, n-pentanol, n-hexanol, 4-methyl-2-pentanol, etc. This solvent can be entirely one of said alcohols or a mixture said alcohols or can be a homogeneous mixture of one or more of said alcohols with up to about 90 percent by volume of another solvent having a low-miscibility with cold water such as a monoor polyhalogenated hydrocarbon having a boiling point between about 40 and about 200 C., e.g., chloroform, methylene chloride, ethylene dichloride, etc. The halogen substituents can be chloro, bromo, iodo, or fluoro. Other solvents that can be employed in mixtures with alcohols include ethers, esters, ketones, aromatic hydrocarbons, etc., which have a low-miscibility with cold water.

In the first extraction step, the solvent to fermentation broth ratio employed is in the range of from about 4:1 to about 1:10, depending on the equipment used, the solvent employed, and the degree of extraction desired. The ratio for batch extraction is usually about 1:1 to about 4:1. The ratio for column countercurrent extraction is usually about 1:2 to about 1.3: 1. A pH in the range of from about four to about 10, preferably about six, is preferred for carrying out the first extraction. The solvent containing extracted solids from the fermentation broth is then concentrated to from about 1 to about 15 percent, preferably about 5 to 7 percent by weight solids content. The concentration step can be carried out by any technique known to those skilled in the art such as evaporation under reduced pressure.

In the second extraction step, the concentrate is introduced into about the center of a multistage fractional liquid extraction column. Simultaneously, water which can optionally be previously equilibrated with the solvent phase is introduced near the top of the column, and a solvent phase optionally in equilibrium with water is introduced near the bottom of the column. The solvent to water ratio is in the range of from about 1:5 to about 1:15, preferably about 1:10. The feed solution to water ratio is in the range of about 1:30. Most of the produce is extracted into the solvent phase which leaves the top of the column.

n-Butanol is the preferred solvent for use in both of the above extraction steps. When n-butanol is employed, about one-half to about 1 percent of the total solids dissolved in the fermentation broth pass into the n-butanol phase. This percentage of the solids contains most of the product.

The above steps of extracting the broth with a solvent, concentrating the solvent extract, and carrying out a fractional liquid extraction of the concentrate can also be carried out by omitting the concentrating step, although this process is much carbon tetrachloride, r

less efficient. Also, the second extraction step above can be omitted, but the yield of product may be decreased somewhat.

The above solvent extract obtained from the fractional liquid extraction column is concentrated by evaporation to a solution or paste containing about 5 to about 20 percent solids; then about 25 to about 50 volumes of n-hcxane are added, and the resulting slurry filtered. The precipitated product is then vacuum-dried to give a solid compound in the form ofa partially purified yellow powder of about 45 to about 75 percent purity. This compound is useful in the same manner as the compounds of formulas I, II, 111, and IV disclosed hereinafter, with dosages adjusted to animal response.

The compound of from about 45 to about 75 percent purity, obtained above, is further purified by one of the following techniques:

a. The 45-75 percent pure compound is partitioned between a solvent system comprising either a chloroformlower alkanol-water system or an ethyl acetate-water system. Examples of solvent systems useful in the practice of the invention include chloroform: isopropanol: water (1:122 V/V mixture), ethylacetate: water 19.5:9), chloroform: isopropanol: ethanol: water (3111125 V/V), chloroform: isopropanol: methanol: water (311.1:5 V/V) etc. The partitioning is carried out in e.g., a Craig countercurrent distribution apparatus, e.g., having 200 tubes, or in an extraction column. When the distribution is carried out in the Craig apparatus, the compound is dissolved in one of the above solvent systems, and placed in one or more of the first tubes of the Craig apparatus. The solutions in those tubes showing a UV maximum at 330-335 mu and significant in vitro activity against Bacillus sp. TA (NRRD Northern Utilization Research and Development Division U.S. Dept. of Agriculture, Peoria, lll. 13-3167) are combined. and the phases separated In place of Bacillus sp. TA, various other organisms can equally well be employed. for example. .rlaplrylrxm'cur aureus, Sarrina lumz, Bacillus" sublilis, Escherichia ml! bacteriophage T-5 etc. The organic solvent phase is evaporated to dryness at a tcmpernture below about 35 C. and the aqueous phase evaporated to a small volume.

also at a temperature below about 35 C. The residues from both phases are combined and lyophilized, afi'ording a compound which is about -90 percent pure.

This material is obtained in purified amorphous form by dissolving the above percent pure compound in a nonalcoholic organic solvent, e.g., acetonitrile, dimethylformamide, dimethylsulfoxide, C -C ketones, such as acetone, etc., and then fractionally precipitating the product by the addition of 1 an aliphatic hydrocarbon, e.g., petroleum ether, hexane, etc.

The 80-90 percent pure compound and the purified amorphous compound are also useful in the same manner as the compounds of formulas 1, 11, Ill, and 1V disclosed hereinafter.

b. The 45-75 percent pure compound is dissolved in methanol in amount to form from about 2 to about 20 percent solution. The solution is filtered, then about 0.05 to about 0.5, preferably about 0.4, volumes of water per volume of methanol are added. The solution is then cooled to a temperature ranging from about -8 C. to about 20 C. The resulting slurry is filtered, optionally dried, and then dissolved in methanol to form from about 1 to about 20 percent, e.g., about 2 percent solution. The solution is filtered and then from about 0.01 to about 0.3, preferably about 0.15, volumes of water per volume of methanol are added slowly with cooling, e.g., at a temperature in a range of from about 8 C. to about 20 C. The crystals which form are filtered, optionally dried, and again dissolved in methanol to form from about 1 to about 20, preferably about 2, percent solution. The solution is treated with activated charcoal, filtered, and then from about 0.01 to about 0.3, preferably about 0.15 volumes of water per volume of methanol are added slowly. The crystalline product obtained consists of a substantially pure compound. Further crystallization from methanol/water as above gives a pure compound of the formula l N. CH. 40 i 6 5 N 2 a ONH, r

5, l 0,1 l ,l la-Tetrahydro-Q-hydroxy-l l-methoxy-8-methyl- -oxo-l H-pyrrolo-[2, l-c l,4 ]-benzodiazepin-2-acrylamide. X is a number from 0 to 1.5.

The above step can also be carried out successfully with an even less pure product, e.g., with a product of only about purity.

The compound of formula 1 or the purified amorphous material obtained by process (a) above can be heated in a nonalcoholic inert solvent, e.g., dimethylsulfoxide, acetonitrile, acetone, etc., boiling from about 50 C. at a temperature in the range of from about 50 to about 200 to form a compound of the formula N WONH:

III

When an alcohol is used as the reactant, the product obtained has the formula OH on,

N CH3 -XH2O wherein R is lower alkyl, phenyl lower alkyl, amino lower alkyl, or a dihydric or polyhydric alcohol residue.

It is to be noted that the compounds of formulas I and IV are significantly more stable than the compound of formula X1] and hence the compounds of formulas l and iv are highly preferred for use in the practice of the invention.

The compounds of formulas l, II, III, and IV are useful as anticancer agents, e.g., they are active against S180 and Ehrlich solid tumors in mice, antiprotozoal agents, e.g., against Endamoeba histolytica and Trichomonas vaginalis, and anthelmintic agents, e.g., against Syphacia obvelata. They can be administered orally or by injection, e.g., in the form of an aqueous solution intravenously, such as by slow intravenous drip of a 0.01 percent aqueous solution. Typical intravenous dosages range from about 0.01 to 0.05 mg./kg. animal body weight,

and typical oral doses are in the range of about 0.2-2.0 mg./kg. animal body weight, with the dosage adjusted to species and individual requirements.

The process of the invention is illustrated by the following examples which are not meant to limit the invention.

EXAMPLE 1 Several loopfuls of spores of Streptomyces .rp. NRRL 3143 are transferred from a mature (2-3 day old) stock agar slant to 100 ml. of germination medium composed as follows in g. per liter:

BACTO tryptone 5 g. BACTO yeast extract 2 g. BACTO soytone 2 g. Soluble starch l0 g. Mannitol 5 g. Magnesium sulfate 7H,O 200 mg. Ferrous ammonium sulfate 6H,0 10 m Zinc chloride 2.l mg. Manganous chloride 4H,O 1.8 mg. Copper sulfate 5H,0 0.3 mg. Cobalt nitrate 6H,O 0.5 mg. Boric acid 0.6 mg.

The medium is contained in a l,000 ml. Pyrex BLAKE bottle. After inoculation the medium is incubated at 45 C., with constant vigorous agitation, on a rotary shaker for 16 hours.

During this period a vigorous growth of the organism ensues.

The contents of two such incubated BLAKE bottles are pooled into a 500 ml. Pyrex inoculum transfer bottle fitted with a tubulature at the bottom and containing 150 ml. of sterile water.

The entire contents of the inoculum transfer bottle are transferred to a gallon stainless steel fermenter which is prepared for it as follows:

To 25 gallons of clean tap water contained in a stainless steel fermenter fitted for controlled agitation, aeration, and temperature control are added the following ingredients:

Grams Potato starch l .500 Enzyme hydrolyzed casein 750 Enzyme hydrolyzed soy protein" 300 Aqueous extract of yeast J00 Mannitol 750 Magnesium sulfate 7H,O 30 Ferrous ammonium sulfate 6H,0 1.5 Zinc chloride 3 l 5 mg. Manganous chloride 4H,O 270 mg. Copper sulfate 5H,0 45 mg. Cobalt nitrate 6l-l,0 75 mg. Boric acid 90 mg. DOW CORNING SILICONE A. emulsion 2.5 g.

SHEFFIELD NZ-AMINE a; "DIFCO BACTO SOYTONE; '"DlFCO BACTO YEAST EXTRACT When all the ingredients are dissolved the volume is brought to 40 gallons (150 liters) with tap water and the pH adjusted to 7.2 with about 60 ml. of 5N potassium hydroxide.

The fermentor is then closed and the contents sterilized by being brought to a temperature of C. and maintained at that temperature from 30-40 minutes. The batch is then cooled to 48 C. and inoculated as described above.

After inoculation the batch is aerated with 3 cubic feet per minute of sterile air and agitated at a shaft speed of 400 r.p.m.; the while maintaining a temperature of 48 C.

Foam is controlled by the addition, as needed, of a sterile 2.5% suspension of DOW SlLlCONE EMULSION AF. About 3,000 ml. of defoamer suspension is used during the batch. Hourly samples are taken aseptically from the 12th hour on and assayed for in vitro potency. The data obtained on the above batch is shown in the table which follows. This batch reaches it maximum potency in 18-20 hours.

Age in Hours l4 l5 l6 l7 l8 I9 10 Broth Potency in Units/ml.

Assay Organism l3 Slaphylurorrus nureur 470 650 800 950 l,l00 l.l00

pH 7.0 6.6 6.5 6.6 6.8 6.7 6.9 7.l

The above process is repeated ten times, the broths obtained are combined, the pH is adjusted to 6, the combined broths are filtered, and the resulting filtrate is extracted coun- 11 tercurrently at the rate of I28 gallons per hour with about the same rate of butanol. in a 12 inch diameter by l 1 ft. high Karr extraction column. A water backwash of 0.2 times the butanol rate is employed at the top of the extraction column to minimize the carryover of water soluble components. The butanol extract is concentrated to approximately a percent solution which comprises the feed to the center of a 3 inch diameter by 20 ft. high Karr fractional liquid extraction column. This column is operated at a water to butanol ratio of about to l, and the butanol extract contains the product. The butanol extract is concentrated by evaporation to a solution or paste containing about 5 to about percent solids; then about to about 50 volumes of n-hexane are added, and the resulting slurry filtered. The precipitated product is then vacuum-dried to give a solid compound.

EXAMPLE 2 A series of fermenters are prepared with the same basic medium and inoculated as described in example 1 except that various commercial sources of enzyme-hydrolyzed soy protein and various sources of whole dried yeast, yeast extract, or yeast autolyzate are used in the medium where hydrolyzed soy protein and aqueous extract of yeast were indicated. All media but one give good broth potencies but some media are noticeably superior, as may be seen from the following table:

3 c.f.m. shaft speed 400 rpm, and the temperature maintained at 48 C. throughout.

The course of the fermentation may be seen from the data in the table which follows.

and yeast additives] Maximum broth potency reached in units/ml.

Sheflield soy T hydrolyzate Amber hydrolyzed soy protein S. Sarcina Bacillus S. Sarcina Bacillus Yeast additive aureus lutea sp. TA aureus lulea 0p. TA

Amber BYF-EO- 980 930 1,200 710 720 820 Amber BYE-300 930 760 1, 400 1, 200 1, 200 1, 900 National grain yeast autolyzate 870 930 1, 400 860 990 1, 400 Besemin Busch 1,100 970 770 1,100 1, 400 1, 200 Standard brands dried brewers yeast 850 890 1, 300 980 020 1, 200 Anheuser Busch dried debittered yeast 700 680 960 1, 100 1, 100 1. 900 Anheuser Busch primary dried yeast Did not support growth. 690 710 1,000

The product is isolated from the above fermentation media according to the process of example i.

EXAMPLE 3 25 gallons of clean tap water are placed into a IOU-gallon fermenter and used to dissolve the following ingredients:

The volume is brought to gallons with tap water and the pH adjusted to 7.2 with 5N potassium hydroxide.

The fermenter is then closed and sterilized by heating to 120 C. for 60 minutes. The batch is cooled to 48 C. and inoculated as described in example i. The air flow is adjusted to Three identical IOU-gallon fermenters are each charged with 40 gallons of nutrient medium, the composition of which is as follows:

Magnesium sulfate heptuhydrate Trace elements-us described in example I.

All butcher are adjusted to pH 7.0 before sterilization. The

tanks are sterilized at 120 C. for one hour. cooled to 48 C. and tanks 2 and 3 are each inoculated with ISO ml. of 18% hour growth taken from a batch of culture NRRL 3l43 developed on the same medium composition and operating conditions as described for example i.

After inoculation, the tanks are each aerated at the rate of 3 cubic feet per minute, agitated at a shaft speed of 400 rpm, and maintained at a temperature of 48 C.

At the l2th hour of incubation tank 2 is adjusted to a pH of 6.8 and acid or alkali is added periodically to maintain the pH between pH 6.7 and 6.9.

Also at the 12th hour, tank 3 is adjusted to pH 7.2 and the pH is maintained between 7.2 and 7.4 for the duration of the fermentation by the addition, as needed, of appropriate amounts of acid or alkali.

The pH of tank I is allowed to go unadjusted.

It can be seen from the data in the following table that pH control both during the fermentation and thereafter is important.

[INFLUENCE OF pH CONTROL OF THE BATCH ON THE YIELD AND STABILITY OF THE ANTIBIOTIC] Broth potency in units (TA) per ml.

Age in hours Tank Number Treatment 12 13 14 15 16 17 18 19 20 21 22 23 24 1 N0 pH adjustment pH of broth 780 1, 1, 000 730 700 630 400 6.9 6.8 6.8 7.1 7.1 7.0 7.3 2 pH maintained at 6.7-6.9 from 12th hour on 3,000 3, 000 2, 900 3, 000 2, 900 3, 200 2, 900 2,700 pH of broth. 6. 8 6. 8 6. 9 6. 7 6. 7 6. 7 6. 7 6. 0 3 pH maintained at 7.2-7.4 from 12th hour on 4, 200 4, 600 4, 300 3,000 2, 700 l, 800 1, 600 1, 600 1 pH of broth. 7. 2 7. 2 7. 3 7. 3 7. 2 7. 2 7. 3 7. 4

EXAMPLES 7 g. of the product prepared by the process of example 1 is dissolved in 350 ml. of chloroform-isopropanol (lzl) which was previously equilibrated with water. This solution is introduced into the center of a l-inch diameter by 20-foot high Kurr extraction column at the rate of 0.5 m|./min. Simultaneously 60 mL/min. of equilibrated aqueous phase is introduced at the bottom of the column and 14.6 ml./min. of equilibrated solvent phase is introduced at the top of the column. Most of the product is extracted into the aqueous phase leaving the top of the column. The aqueous phase is reextracted countercurrently in a l-inch diameter by -foot high extraction column employing a 1:1 isopropanol-chloroform solvent at a solvent to water ratio of 1:1. The product passes into the isopropanolchloroform solvent which leaves at the bottom of the extraction column. This solution is concentrated to 58 ml., filtered, and then treated with 2.9 liters of technical hexane to precipitate the product. The product is filtered and dried.

The dried product which is 90 percent pure is crystallized from acetone to yield a highly active purified material.

EXAMPLE 6 g. of the product prepared according to example i was distributed between 120 ml. each of upper and lower phases of a solvent system consisting of isopropanol: chloroform: water 1:112). The phases were then introduced into the first three tubes of a 200-tube Craig countercurrent distribution apparatus and run at room temperature for 197 transfers. The upper and lower phases of tubes 45 to 75 were combined, the organic phase evaporated at a temperature below C. in vacuo and the residue added to the corresponding aqueous phase, and the aqueous phase lyophylized. The lyophylized residue was crystallized from acetone to yield a purified material.

EXAMPLE 7 200 g. of the product prepared according to example I is dissolved in 4,000 ml. of methanol and the solution filtered. The filtrate is agitated and 332 ml. of water added during the course of 1 hour. The temperature during the addition is maintained at 22 C. The solution is then cooled to 0 C. in 1 hour and then stirred overnight in a cooled bath maintained at 9 C. Then the resulting slurry is filtered. washed twice with a minimum quantity of aqueous methanol (8.3 volume/volume percent H 0), and dried in a vacuum dessicator at room temperature. 86.9 g. of dark brown precipitate is obtained.

The above precipitate is dissolved in 4,340 ml. of methanol, filtered, and 672.7 ml. of water slowly added over a period of 3 hours at a temperature of 0 C. The resulting mixture is then placed in a cooled bath at 9 C. and then stirred overnight. The crystals are then filtered off, washed with a minimum of aqueous methanol at 20 C. (15.5 volume/volume percent H 0) and vacuum dried at room temperature, 69.8 g. of a yellow needlelike crystalline solid is obtained. The crystalline solid is again dissolved in 4,340 ml. of methanol, 6.95 g. of act ivated charcoal (NORITE 56) are added with stirring and after 10 minutes at room temperature filtered off and the filtrate treated with 672.7 ml. of water added slowly over a period of 3 hours at 0 C. The mixture is then placed in a cooled bath at 9 C. and stirred overnight. The resulting crystals are filtered, washed with a minimum of aqueous methanol at 20 C. andvacuum dried at room temperature. 59.6 g. of a light yellow crystalline product of formula I is obtained.

III

The product of formula I was recrystallized from acetonitrile to prepare the corresponding anhydrous compound of the formula 0H OCHn Ulla /N ONH; Ill

EXAMPLE8 3 g. of the compound of formula I obtained in example 7 is dissolved in 600 ml. of acetonitrile. The resulting solution is concentrated by distillation at atmospheric pressure to a small volume (about 200 ml.). A crystalline solid is obtained which is again dissolved in 450 ml. of acetonitrile and the resulting solution is concentrated by distillation at atmospheric pressure to about ml. The compound of formula II crystallizes out, melting point 205-206 dec. (vac.

EXAMPLE 9 0.1 g. of the compound of formula ll obtained in the above example 8 is dissolved in 50 ml. of boiling acetonitrile. An excess of water was added and the mixture allowed to stand for l hour at room temperature. The resulting solution is concentrated by distillation to a small volume at room temperature under vacuum. 0n standing, crystals of the compound of formula III are obtained which melt at l88-l88 dec. (vac):

OH OH N OH3- CONH, 1n

EXAMPLEIO 65 mg. of the compound of formula ll obtained in example 8 above is dissolved in 15 ml. of n-butanol at room temperature. The resulting clear solution is concentrated to a small volume at room temperature under high vacuum. The residue is treated with 30 ml. of n-hexane. A product having the formula f ownmcn,

precipitated out, melting point l55-l75 C. with decomposition (vac).

EXAMPLE 1 l 0.2 g. of the compound of formula II obtained in example 8 above is dissolved in l00 ml. of boiling acetonitrile and 5 ml.

of benzyl alcohol added thereto. The resulting solution is allowed to stand for 3 hours at room temperature. The acetonitrile is removed under vacuum at room temperature. The residue is treated with 100 ml. of ether. A product having the formula CONH, Vl

precipitates out, melting point lO8-l09 C.

In the specification, the terms unit/ml" or units/mL," e.g. referring to broth potency, are to be understood as follows: units/ml is the value arbitrarily assigned to an aqueous solution which produces an 18-22 mm. diameter zone of inhibited growth in the known cup plate agar diffusion assay when either Staphylococcus aureus or Bacillus sp. TA is used as the test organism.

We claim:

1. A process for the preparation of a pharmacologically active material comprising the steps of:

1. cultivating with agitation and aeration a thermophilic Streptomycete of the species rufuineus var. thermotolerans, having an NRRL number selected from the group consisting of 3143 and 3144 in nutrient media comprising:

a. from about 0.1 to about 9.0 percent by weight of a protein source wherein the ratio of total nitrogen to amino nitrogen is greater than three and wherein the total nitrogen is in the range of from about 0.005 to about 0.48 percent weight/volume; and

b. a carbohydrate source;

and wherein the staring pH of the nutrient media is in the range of from about six to about 8.5 at a temperature in the range of from about 35 to about 55;

2. adjusting the pH after about 12 to about 15 hours of fermentation to a pH in the range of about 6.0 to about 6.9;

3. treating the resulting fermentation broth with an extraction solvent comprising a monohydric saturated aliphatic alcohol having a boiling point up to about 200 C. and which has a low-miscibility with cold water to form an extraction solvent containing nonvolatile dissolved materia1; and isolating said nonvolatile dissolved material therefrom.

2. A process according to claim 1 wherein said fermentation broth is filtered, and the filtrate therefrom instead of the fer mentation broth is extracted according to step 3.

3. A process according to claim 1 wherein said extraction solvent containing nonvolatile dissolved material is concentrated and the resulting concentrate treated with water and a solvent comprising a monohydric saturated aliphatic alcohol having a boiling point up to about 200 C. which has a low miscibility with cold water by fractional liquid extraction. and removing said extraction solvent from said nonvolatile dissolved material.

4. A process according to claim 1 wherein said extraction solvent is n-butanol.

5. A process for the preparation of pharmacologically active material comprising the steps of:

1. culturing with agitation and aeration a thermophilic Slreptomycete of the species refuineus var. thermoralerans and having a NRRL number selected from the group consisting of 3143 and 3144 in a nutrient medium having the following characteristics:

a. from about 1.0 to about 5.0 percent by weight of a protein source selected from the group consisting of peptonized milk, dried milk, skim milk, enzymatic hydrolysates of soy, peanut, yeast, and fish proteins, and mixtures thereof, wherein the ratio of total nitrogen to amino nitrogen is greater than three and wherein the total nitrogen is in the range of from about 0.015 to about 0.20 percent weight/volume; and

b. a carbohydrate source;

and said nutrient media having a starting pH of from about 6.7 to about 7.3, at a temperature in the range of from about 40 to about 50 C.;

2. adjusting the pH after about 12 to about 15 hours of fermentation to a pH in the range of about 6.0 to about 6.9;

3. treating the resulting fermentation broth with n-butanol in the range of from about 4:1 to about 1:10 n-butanol to fermentation broth to form a solution of n-butanol and nonvolatile dissolved material;

4. concentrating the n-butanol solution to form about 1 to about 15 percent by weight nonvolatile material content;

5. fractionally extracting the resulting n-butanol concentrate with water and n-butanol at an n-butanol concentrate to water ratio of about 1:5 to about 1:15 in a fractional liquid extraction column; and

6. removing the n-butanol from the nonvolatile pharmacologically active material.

a tars! 

2. A process according to claim 1 wherein said fermentation broth is filtered, and the filtrate therefrom instead of the fermentation broth is extRacted according to step
 3. 2. adjusting the pH after about 12 to about 15 hours of fermentation to a pH in the range of about 6.0 to about 6.9;
 2. adjusting the pH after about 12 to about 15 hours of fermentation to a pH in the range of about 6.0 to about 6.9;
 3. treating the resulting fermentation broth with an extraction solvent comprising a monohydric saturated aliphatic alcohol having a boiling point up to about 200* C. and which has a low-miscibility with cold water to form an extraction solvent containing nonvolatile dissolved material; and isolating said nonvolatile dissolved material therefrom.
 3. treating the resulting fermentation broth with n-butanol in the range of from about 4:1 to about 1:10 n-butanol to fermentation broth to form a solution of n-butanol and nonvolatile dissolved material;
 3. A process according to claim 1 wherein said extraction solvent containing nonvolatile dissolved material is concentrated and the resulting concentrate treated with water and a solvent comprising a monohydric saturated aliphatic alcohol having a boiling point up to about 200* C. which has a low miscibility with cold water by fractional liquid extraction, and removing said extraction solvent from said nonvolatile dissolved material.
 4. A process according to claim 1 wherein said extraction solvent is n-butanol.
 4. concentrating the n-butanol solution to form about 1 to about 15 percent by weight nonvolatile material content;
 5. fractionally extracting the resulting n-butanol concentrate with water and n-butanol at an n-butanol concentrate to water ratio of about 1:5 to about 1:15 in a fractional liquid extraction column; and
 5. A process for the preparation of pharmacologically active material comprising the steps of:
 6. removing the n-butanol from the nonvolatile pharmacologically active material. 